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WO2012163663A1 - Procédé et dispositif pour produire un ciment clinker - Google Patents

Procédé et dispositif pour produire un ciment clinker Download PDF

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Publication number
WO2012163663A1
WO2012163663A1 PCT/EP2012/058939 EP2012058939W WO2012163663A1 WO 2012163663 A1 WO2012163663 A1 WO 2012163663A1 EP 2012058939 W EP2012058939 W EP 2012058939W WO 2012163663 A1 WO2012163663 A1 WO 2012163663A1
Authority
WO
WIPO (PCT)
Prior art keywords
heat
heat exchanger
transfer fluid
flue gas
clinker
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2012/058939
Other languages
German (de)
English (en)
Inventor
Helmut Leibinger
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Suedbayerisches Portland-Zementwerk Gebr Wiesbock & Co GmbH
Original Assignee
Suedbayerisches Portland-Zementwerk Gebr Wiesbock & Co GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=46085048&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2012163663(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Suedbayerisches Portland-Zementwerk Gebr Wiesbock & Co GmbH filed Critical Suedbayerisches Portland-Zementwerk Gebr Wiesbock & Co GmbH
Priority to EP12720882.5A priority Critical patent/EP2545337B1/fr
Priority to DK12720882.5T priority patent/DK2545337T3/da
Publication of WO2012163663A1 publication Critical patent/WO2012163663A1/fr
Priority to US14/091,097 priority patent/US9873635B2/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/343—Heat recovery
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories or equipment specially adapted for rotary-drum furnaces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/10—Arrangements for using waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/20—Arrangements for treatment or cleaning of waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0233—Other waste gases from cement factories

Definitions

  • the invention relates to a device or a method according to the preambles of the independent claims, in particular a device for producing cement clinker, which is also referred to as clinker.
  • the device has a furnace for burning raw meal to clinker. From an outlet of the stove exit flue gases.
  • the necessary to implement the nitrogen oxides reaction temperature can by catalysts of, for example titanium dioxide (Ti0 2), tungsten trioxide (W0 3) or vanadium pentoxide (V 2 0 5) reduction pieces are sheet.
  • catalytic denitrification designated also known as SCR, which stands for "Selective Catalytic Reduction” - in German selective catalytic reduction.
  • SCR Selective Catalytic Reduction
  • SNCR Selective Non Catalytic Reduction
  • the flue gases of the stove are dust-laden and emerge from the kiln on the order of 900 - 1100 ° C. These flue gases are then used to preheat and deacidify the raw meal in so-called raw meal preheaters. These are usually used cascaded cyclone separator, which are usually arranged in heat exchanger towers. The flue gases leaving the raw meal preheater would have a temperature sufficient for SCR denitrification, but would still be laden with fine dust which has an abrasive effect on the catalyst and can lead to clogging of the catalyst. Therefore, it is appropriate to dedust the flue gases before the SCR denitrification.
  • hot gas filters Although there are filters with which you could dedust about 450 ° C hot gases, so-called hot gas filters, but these are expensive and bulky. It is easier to use so-called bag filters, but they require significantly lower flue gas temperatures, so that when they are used, the flue gases must first be cooled, then filtered and then heated again to the temperature necessary for the catalytic reduction. This arrangement is also referred to as a "low-dust" or "tail-end" configuration.
  • DE 10 2010 004 011 B3 discloses a method and a plant for the production of cement clinker. This has as usual a rotary kiln exit from the exhaust.
  • the exhaust gases are fed to a raw meal preheater, emerge from this and are de-nitrogenized in a downstream SCR catalyst.
  • the exhaust gas is first cooled in a cooling tower a, then dedusted in a filter and then heated in a heat exchanger to the optimum temperature for the SCR catalyst.
  • the heat exchanger on the hot side of the heated by the SCR denitrification flue gas is supplied.
  • the heat exchanger is thus a recuperator.
  • EP 0 461 305 B1 discloses a process for purifying the exhaust gases of plants for the production of cement clinker and a corresponding plant.
  • the plant has a rotary kiln, the exhaust gases of a heat exchanger tower for Raw meal preheating be supplied. Subsequently, the exhaust gases feed either a raw material mill or a cooling tower and are then brought together again and fed to a multi-stage filter system.
  • the first filter is a dust filter designed as an electrostatic filter. This is followed by a second filter stage with three filter chambers designed as packed bed reactors. Before both filter stages the flue gas stream fresh air is added, causing the flue gases cool.
  • the invention has for its object to reduce the loss of energy in the production of clinker.
  • the heat generated in the furnace can be used particularly efficiently and versatile because heat generated in the furnace is transferred to a heat transfer fluid via a first heat exchanger, the heat transfer fluid with the heat through at least one conduit is transported at least a second heat exchanger, then delivered to a heat sink, eg to heat a flue gas stream to a temperature necessary for its denitrification.
  • the heat can, for example, be used to heat, which was initially produced in the oven, but then, for example, is carried out with the clinker therefrom. to heat flue gases to a temperature necessary for an SCR after dedusting.
  • the exhaust air of a clinker cooler by means of the first heat exchanger withdraw heat and thereby heat the heat transfer fluid.
  • This heat transfer fluid is then conveyed to a heat sink and then gives at least a portion of the heat to the second heat sink via the second heat exchanger.
  • the second heat sink can be, for example, a dedusted flue gas stream, which is then fed to an SCR plant for denitrification.
  • the device for producing clinker has at least one furnace for
  • Burning raw meal to clinker with at least one outlet for flue gases e.g. a rotary kiln and means for de-stoking flue gases leaving the kiln, e.g. an SCR system.
  • a first heat exchanger serves to supply at least one heat transfer fluid to the heat produced in the furnace during the combustion process.
  • the heat transfer fluid is transported via at least one line for the heat transfer fluid to at least a second heat exchanger to heat the flue gases in the second heat exchanger with previously supplied to the heat transfer fluid heat, to subsequently de-embroider.
  • the device has means for supplying the heated flue gases to the de-stemming means.
  • the heat source with which the flue gases can reach a temperature necessary for denitrification can be used. be heated and the location of the flue gas heating spatially separated, without having to accept large heat losses in purchasing. Therefore, one gains an additional degree of freedom in the demand-based distribution of the heat generated in the furnace. This allows a better use of the heat generated in the furnace as process heat, especially for secondary processes in the clinker production.
  • Heat can z. B. be transferred in a heat exchanger partly to another substance with a lower temperature. Heat can be transferred from one substance to another substance and transported by the transport of substances, eg by a stream of fluid with the stream. In such processes, the term heat refers to the thermal energy transmitted or transported in a time interval.
  • the invention is based on the observation that the heat generated in the furnace is literally transported away from the kiln by two processes: on the one hand through the hot clinker and on the other hand through the hot flue gases.
  • the device preferably has at least one clinker cooler, on which the hot clinker is deposited.
  • the clinker cooler has at least one coolant tap for drawing off heated coolant through the hot clinker and supplying it to the first heat exchanger, whereby heat stored in the coolant is supplied to the heat transfer fluid.
  • the process is particularly economical when the heat transfer fluid circulates in a cycle.
  • As sauceträgefluid is preferably used a so-called thermal oil. This is a high boiling temperature resistant liquid.
  • At least one filter for example a bag filter, is preferred in the flue gas stream upstream of the first heat exchanger. This increases the service life of the catalyst for SCR denitrification.
  • a third heat exchanger is preferably arranged in the flue gas stream to cool flue gas to a temperature compatible with the filter and in turn to heat at least a second heat transfer fluid. More heat can be supplied to the second heat transfer fluid than is necessary for the subsequent heating of the flue gas for the SCR denitrification, because the temperature of the flue gas stream after leaving the usual raw meal preheating is about 200 ° C higher than that at the inlet of the Catalyst for the SCR necessary temperature.
  • the heat stored in the second heat transfer fluid is therefore preferably used as process heat for other processes, e.g. to operate a steam turbine.
  • the third heat exchanger can thus have in particular at least one steam boiler.
  • the device has a further heat exchanger, which is connected to the means for Entsticken and the second heat exchanger such that heat of the emerging from the means for Entsticken flue gases in the second heat exchanger entering flue gases.
  • This heat exchanger will be referred to hereinafter as well for reasons of clarity of reference Recuperator designated.
  • the device preferably has means for directing de-expanded flue gases to a further heat exchanger in order to heat another heat carrier fluid with the heat of the flue gas, for example as feedwater preheating for a steam boiler.
  • This further heat exchanger is preferably arranged subordinate to the above-described recuperator in the denitrified flue gas stream.
  • the outlet temperature of the flue gas at the outlet of the further heat exchanger is preferably greater than or equal to about 100 ° C, preferably about 110 ° C, because below this temperature in the flue gas contained water condenses in which gases such as HCl, H 2 S0 4 and others solve what leads to the formation of acid in the device which attacks lines, eg as part of a chimney.
  • the first heat exchanger has at least one line for the heat transfer fluid and at least one further line for heating a further heat transfer fluid, e.g. a feed fluid for a steam boiler.
  • a further heat transfer fluid e.g. a feed fluid for a steam boiler.
  • the further line of the first serves
  • Heat exchanger of the preheating of the second heat transfer fluid which is supplied after preheating by a line to the third heat exchanger, for example, said steam boiler to heat it there further.
  • This improvement makes use of the observation that the minimum temperature for common SCR processes depends on the flue gas composition, but is typically of the order of 230-270 ° C. This temperature is the minimum temperature for the heat carrier fluid flowing to the first heat exchanger. Consequently, the temperature of the heat carrier, the heat transfer After the heating of the heat transfer fluid, the fluid in the first heat exchanger does not become colder than this minimum temperature for the SCR.
  • the subordinate line for heating a feed fluid in the simplest case, for example, water, the heat carrier can be withdrawn further usable heat.
  • the heat carrier may be, for example, a previously heated by clinker coolant.
  • the furnace may have a branch for flue gases to remove impurities present in the raw meal, such as chlorides, sulfur, alkali metals from the circuits between the furnace and raw meal preheater.
  • the first heat exchanger may be connected to the branch such that at least a portion of the branched flue gas stream is supplied to the first heat exchanger to supply heat stored in the flue gas stream to the heat transfer fluid.
  • the flue gas stream is cooled.
  • the cooled flue gas stream can then be used for example as cooling air for a clinker cooler and be returned to the oven.
  • the cooled flue gas partial stream can also be added to the remaining flue gases downstream of the raw meal preheater.
  • the furnace is connected to the exhaust side with at least one raw meal preheater to preheat and at least partially deacidify the raw meal with heat stored in the flue gases.
  • the first heat exchanger may be provided with a flue gas outlet of the raw meal preheater be connected that exiting the raw meal preheater flue gas heats the heat transfer fluid.
  • the single drawing shows an example of a flow chart of a device for burning clinker from raw meal.
  • Core of the device is a rotary kiln 10 between a clinker cooler 20 and a heat exchanger tower 30.
  • the rotary kiln 10 has a projecting from the side of the clinker cooler in the rotary kiln burner 10 (not shown) to the heat required for the production of clinker by combustion in the Rotary kiln 10 to produce.
  • the resulting during combustion flue gas exits heat exchanger tower side of the rotary kiln 10 from. From this side, in return raw meal is introduced into the rotary kiln 10.
  • the heat exchanger tower 30 has here exemplarily 4 cascaded interconnected, that is connected in series cyclones 32, for preheating and partial deacidification of raw meal by heat of the flue gas and coarse dedusting of the flue gas.
  • the flue gas leaving the heat exchanger tower 30 has a typical temperature of 300-500 ° C.
  • a flue gas filter 50 Before the flue gas is fed to a flue gas filter 50 for further dedusting, it is cooled to a temperature smaller than 150 ° C.
  • heavy metals contained in the flue gas such as: mercury and thallium, condense on the dust contained in the smoke. This dust is deposited in the flue gas filter 50, it thus acts as a cold trap for heavy metals.
  • the volume to be dedusted (per unit of time) is drastically reduced and cost-effective fabric filter technology can be used.
  • flaps 38 are provided to divide the flue gas flow on the three possibilities for cooling. In normal operation as little as possible, so no or almost no flue gas should be cooled by means of the evaporative cooler 36, because the heat extracted from the flue gas in the evaporative cooler 36 is no longer available as process heat available.
  • the evaporative cooler thus preferably has only the function of an emergency cooler, if the steam boiler 100 can not be used.
  • the cooled flue gas is then dedusted in a flue gas filter 50 and the dedusted flue gas is fed to an SCR unit 60 for the catalytic denitrification of the flue gases. It must be heated to at least 230 ° C-270 ° C. For this reason, it is first fed from the flue gas filter 50 to a recuperator 62, to which flue gas escaping in countercurrent from the SCR unit is supplied, so that heat is transferred from the de-embossed (pure gas) to the flue gas (crude gas) to be de-stiffened , The flue gas leaving the recuperator and to be de-stiffened is fed to another heat exchanger in order to heat it up further.
  • this further heat exchanger 64 is also referred to as a "second heat exchanger.”
  • the heat required for heating the flue gas is supplied to the second heat exchanger 64 via a so-called thermal oil as the heat carrier fluid
  • Stage recuperator 62, second stage “second heat exchanger 64" heated flue gas is fed to the SCR unit 60 and entstickt there.
  • the heat extracted from the flue gas in the heat exchanger 102 serves to feed water for the boiler 100 and / or boilers 110. Alternatively, it could also be fed into a district heating network or be used in an ORC process for power generation Common abbreviation for "Organic Rankine Cycle", a process in which steam turbines are operated with the steam of low-boiling organic fluids.
  • heat is removed from the rotary kiln 10 with the preferably continuous removal of clinker from the rotary kiln 10.
  • This first about 1450 ° C hot clinker is cooled in the clinker cooler 20.
  • the coolant used is preferably air.
  • the clinker cooler 20 is thus a heat exchanger.
  • a portion of the air heated in the clinker cooler 20 is removed via a so-called center air tap 24 from the clinker cooler.
  • exhaust air stored heat
  • the thermal oil is heated as a heat transfer fluid after a heavy dust dusting by a cyclone 77 in a heat exchanger 80.
  • the heat transferred to the heat transfer fluid can also be transported over long distances with only slight heat losses, in particular in order to heat the flue gas to be denitrified in the second heat exchanger 64 to the temperature necessary for denitrification.
  • the heat exchanger 80 has an inlet 81 for the exhaust air, which is first passed in the heat exchanger via a first line 83 to heat the heat transfer fluid flowing through the first conduit. Subordinate to the first line 83, a second line 84 is arranged, via which the exhaust air is passed. In the second line 84 flows another heat transfer fluid and is heated by the exhaust air. In the example shown, the further heat transfer gerfluid water, which is preheated as feed water for the boiler 100 and / or a boiler 110. The exhaust air leaves the heat exchanger 80 via an outlet 82. The exhaust air is guided in the heat exchanger 80 in a flow channel.
  • the flow channel is U-shaped, ie it has two free legs 85, 86, which are connected by a transverse leg below 87. In each of the two free legs 85, 86 is ever one of the two lines 83, 84. By deflecting the exhaust air in the region of the transverse leg 87 collects at the bottom of the transverse leg of the exhaust air mit Processer clinker dust, which can be deposited there.
  • the outlet 85 is connected to a cooler 70 to adjust the temperature for the downstream filter 75. With the filter 75, the exhaust air is dedusted and can be discharged eg via an indicated fireplace.
  • the device for burning clinker has in addition to the above-described flue gas treatment a so-called chloride bypass.
  • Part of the flue gas leaving the rotary kiln 10 is not fed to the raw meal preheater, but first mixed with fresh air in a mixing chamber 90.
  • a mixing temperature of about 450 ° C (400 ° C-500 ° C) is set. This temperature achieved allows a hot gas dedusting in a hot gas filter 94.
  • the hot gas filter is followed by a boiler 110 downstream. Steam is generated in the boiler, which is expanded in the turbine assembly.
  • the emerging from the boiler flue gas is used as cooling air for the clinker cooler 20 and fed via the clinker cooler 20 back into the rotary kiln 10. Because the flue gases leaving the boiler still have a temperature that is significantly above normal ambient temperatures, the return of the flue gases via the clinker cooler can achieve a very high secondary air temperature, and the fuel consumption drops correspondingly.
  • coolers here for example air / air heat exchanger

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Biomedical Technology (AREA)
  • Ceramic Engineering (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Chimneys And Flues (AREA)

Abstract

L'invention concerne un dispositif pour réaliser la combustion de clinker dans un four (10). Il est possible d'utiliser la chaleur générée dans le four (10) de manière particulièrement efficace et variée, lorsque la chaleur générée dans le four est transférée à un fluide caloporteur par l'intermédiaire d'un premier échangeur thermique (80), et que le fluide caloporteur et la chaleur transférée sont transportés dans au moins une conduite vers au moins un deuxième échangeur thermique (64) pour délivrer la chaleur au niveau d'un dissipateur thermique, par exemple pour chauffer un flux de gaz de combustion afin de le porter à une température nécessaire à sa dénitruration.
PCT/EP2012/058939 2011-05-27 2012-05-14 Procédé et dispositif pour produire un ciment clinker Ceased WO2012163663A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP12720882.5A EP2545337B1 (fr) 2011-05-27 2012-05-14 Procédé et dispositif pour produire un ciment clinker
DK12720882.5T DK2545337T3 (da) 2011-05-27 2012-05-14 Fremgangsmåde og indretning til fremstilling af cementklinker
US14/091,097 US9873635B2 (en) 2011-05-27 2013-11-26 Method and device for producing cement clinker

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102011050677.2A DE102011050677B4 (de) 2011-05-27 2011-05-27 Vorrichtung und Verfahren zur Herstellung von Zementklinker
DE102011050677.2 2011-05-27

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US14/091,097 Continuation US9873635B2 (en) 2011-05-27 2013-11-26 Method and device for producing cement clinker

Publications (1)

Publication Number Publication Date
WO2012163663A1 true WO2012163663A1 (fr) 2012-12-06

Family

ID=46085048

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2012/058939 Ceased WO2012163663A1 (fr) 2011-05-27 2012-05-14 Procédé et dispositif pour produire un ciment clinker

Country Status (5)

Country Link
US (1) US9873635B2 (fr)
EP (1) EP2545337B1 (fr)
DE (1) DE102011050677B4 (fr)
DK (1) DK2545337T3 (fr)
WO (1) WO2012163663A1 (fr)

Cited By (1)

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DE102013020815A1 (de) * 2013-12-17 2015-06-18 Walter Würzinger Kontinuierliche Verfahrensanlage für energieeffiziente industrielle Öfen mittels gekoppeltem Dampfkraftprozess und Restsauerstoff-Optimierung

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DE102009041089C5 (de) * 2009-09-10 2013-06-27 Khd Humboldt Wedag Gmbh Verfahren und Anlage zur Herstellung von Zement mit verringerter CO2-Emission
DE102012020300B4 (de) * 2012-10-17 2016-05-12 Khd Humboldt Wedag Gmbh Verfahren zur Nutzung der Abwärme einer Anlage zur Herstellung von Zement und Anlage zur Herstellung von Zement
EA201592181A1 (ru) * 2013-06-07 2016-07-29 Милли Спановиц Устройство и способ переработки отходов с возможностью выбора качества выпускаемых продуктов
DE102014100896A1 (de) * 2014-01-27 2015-07-30 Thyssenkrupp Ag Verfahren zur Wärmebehandlung eines Stoffstroms und zur Reinigung von dabei entstehenden Abgasen
AT14170U1 (de) * 2014-05-27 2015-05-15 Scheuch Gmbh Vorrichtung zur Herstellung von Zementklinker
ES2665331T3 (es) 2016-03-18 2018-04-25 Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH Línea de clínker de cemento y procedimiento para operar una línea de clínker de cemento
DK3219689T4 (da) 2016-03-18 2022-07-04 Suedbayerisches Portland Zementwerk Gebr Wiesboeck & Co Gmbh Cementklinkerlinie og fremgangsmåde til drift af en cementklinkerlinie
DE102016207313A1 (de) * 2016-04-28 2017-11-02 Thyssenkrupp Ag Anlage zur Herstellung von Zement oder Aufbereitung von Erzen und Verfahren zum Betreiben einer solchen Anlage
AT519060B1 (de) 2016-09-09 2018-07-15 Baumit Beteiligungen Gmbh Verfahren zum Brennen von Kalk oder Zement mit Synthesegas
CN110455091A (zh) * 2019-09-16 2019-11-15 中国科学院过程工程研究所 一种用于水泥烟气的scr脱硝系统
CN111288808A (zh) * 2019-11-15 2020-06-16 中建材科创新技术研究院(山东)有限公司 水泥窑旁路放风余热烟气利用装置及其利用方法
AT17408U1 (de) * 2021-03-24 2022-03-15 Scheuch Man Holding Gmbh Vorrichtung und Verfahren zur Herstellung von Zementklinker
US20240426552A1 (en) * 2021-09-08 2024-12-26 Loesche Gmbh Clay calcining plant

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US9873635B2 (en) 2018-01-23
EP2545337A1 (fr) 2013-01-16
DE102011050677A1 (de) 2012-11-29
US20140087319A1 (en) 2014-03-27
EP2545337B1 (fr) 2013-07-31
DK2545337T3 (da) 2013-11-04
DE102011050677B4 (de) 2014-08-28

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